CN102329651B - Three-stage gasification device for producing synthesis gas through biomass pyrolysis and gasification - Google Patents
Three-stage gasification device for producing synthesis gas through biomass pyrolysis and gasification Download PDFInfo
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Abstract
本发明提供了一种三段式生物质热解气化制取合成气的气化装置。主体为反应炉，采用圆柱形或方形结构，其内部上段热解炉膛为生物质热解反应室，下段气化炉膛为热解产物的水蒸汽流化气化室，而反应炉的中部炉膛设有环状的催化剂床层(催化裂解气化室)。所述上段热解炉膛设有进料装置，上段热解炉膛与下段气化炉膛连通。下段气化炉膛底部设置有混合气进气口。反应炉炉体上端设置有烟气出气口，烟气出气口连接有旋风分离器。反应炉外侧对应分别设置有控温装置。本发明简化了整个合成气制备的实验系统，提高了气化炉的产气率及合成气的品质，减少了产气中焦油的含量水平。本发明装置具有控温方便，节能环保，运行连续，结构简单等优点。
The invention provides a three-stage biomass pyrolysis gasification gasification device for producing synthesis gas. The main body is a reaction furnace with a cylindrical or square structure. The upper pyrolysis furnace inside is a biomass pyrolysis reaction chamber, the lower gasification furnace is a water vapor fluidized gasification chamber for pyrolysis products, and the middle furnace of the reaction furnace is set There is an annular catalyst bed (catalytic cracking gasification chamber). The upper pyrolysis furnace is provided with a feeding device, and the upper pyrolysis furnace communicates with the lower gasification furnace. A mixed gas inlet is provided at the bottom of the gasification furnace in the lower section. The upper end of the reaction furnace body is provided with a flue gas outlet, and the flue gas outlet is connected with a cyclone separator. The outside of the reaction furnace is respectively equipped with temperature control devices. The invention simplifies the whole experimental system for synthesis gas preparation, improves the gas production rate of the gasification furnace and the quality of the synthesis gas, and reduces the tar content level in the produced gas. The device of the invention has the advantages of convenient temperature control, energy saving and environmental protection, continuous operation, simple structure and the like.
Description
技术领域 technical field
本发明属于生物质能源化工技术领域，特别涉及一种三段式生物质热解气化制取合成气的气化装置。The invention belongs to the technical field of biomass energy chemical industry, and in particular relates to a gasification device for producing syngas by three-stage biomass pyrolysis gasification.
技术背景 technical background
生物质是通过光合作用而形成的各种有机体，它直接或间接地来源于绿色植物的光合作用，可转化为常规的固态、液态和气态燃料，它分布广泛、可利用量大，是一种可再生能源，并且也是唯一一种可再生的含有碳氢组分和热能的、可储存的自然原料，利用生物质进行能源利用和化工生产，具有CO2零排放的特征。随着传统化石能源储量的日益减少，以及由于使用化石能源带来的环境污染问题，重视和发展可再生、环保能源已成为各国政府的共识。通过热化学、生物化学等方法，能够将生物质转变为清洁的气体或液体燃料，生产合成柴油/汽油、化工产品以及满足电力需求等等，具有全面替代化石能源的潜力，成为世界各国优先发展的新能源。Biomass is a variety of organisms formed through photosynthesis. It is directly or indirectly derived from the photosynthesis of green plants and can be converted into conventional solid, liquid and gaseous fuels. It is widely distributed and available in large quantities. It is a kind of Renewable energy, and also the only renewable natural raw material that contains hydrocarbon components and heat energy, can be stored, uses biomass for energy utilization and chemical production, and has the characteristics of zero CO2 emissions. With the decrease of traditional fossil energy reserves and the environmental pollution caused by the use of fossil energy, it has become the consensus of governments to attach importance to and develop renewable and environmentally friendly energy. Through thermochemical, biochemical and other methods, biomass can be converted into clean gas or liquid fuels, synthetic diesel oil/gasoline, chemical products, and electricity demand can be produced, etc., which has the potential to fully replace fossil energy, and has become a priority development of countries around the world. of new energy.
将生物质转变为清洁气体或液体燃料的方法很多，其中，生物质热化学转化技术与其它技术相比能够适应所有的生物质种类，且具有大型工业化生产的能力，易于规模化应用。生物质热解气化制备合成气(主要成分为H2和CO气体)，进而合成液体燃料(如甲醇、乙醇、二甲醚、烯烃、柴油和石脑油等)是热化学转化技术中最具有发展前景的生物质能源资源化利用途径之一，受到了国内产业界和学术界前所未有的重视，并投入了大量的人力和物力进行相关的研究和开发，其中通过利用秸秆、稻壳、木柴等生物质原料通过高温热化学方法制备含有氢气和一氧化碳的合成气的技术已经得到广泛的研究。生物质热解气化制备合成气工艺中气化反应器是其核心设备。气化反应器的形式、结构、运行的工艺参数对产品合成气的品质有直接影响。因此，开发高效生物质热解气化装置制取高品质合成气，并经后续合成反应器转化为液态烃类、醇类和醚类等燃料，既可以缓解对国际原油市场的依赖，也可以减少国内传统化石能源的消耗，同时具有积极保护环境的社会效益。There are many ways to convert biomass into clean gas or liquid fuels, among which, compared with other technologies, biomass thermochemical conversion technology can adapt to all types of biomass, and has the ability of large-scale industrial production, and is easy to apply on a large scale. Biomass pyrolysis gasification to produce synthesis gas (mainly composed of H2 and CO gas), and then to synthesize liquid fuels (such as methanol, ethanol, dimethyl ether, olefins, diesel oil and naphtha, etc.) is the most advanced thermochemical conversion technology. One of the promising approaches to resource utilization of biomass energy has received unprecedented attention from the domestic industry and academia, and a lot of manpower and material resources have been invested in related research and development. The technology of producing synthesis gas containing hydrogen and carbon monoxide by high-temperature thermochemical method from biomass raw materials has been extensively studied. The gasification reactor is the core equipment in the synthesis gas production process of biomass pyrolysis gasification. The form, structure, and operating process parameters of the gasification reactor have a direct impact on the quality of the product synthesis gas. Therefore, the development of high-efficiency biomass pyrolysis gasification equipment to produce high-quality syngas, which is converted into fuels such as liquid hydrocarbons, alcohols, and ethers through subsequent synthesis reactors, can not only alleviate the dependence on the international crude oil market, but also Reduce the consumption of domestic traditional fossil energy, and at the same time have the social benefits of actively protecting the environment.
目前用于生物质气化的气化反应器(气化炉)大致可以分为三种：固定床、气流床和流化床。固定床气化炉的结构简单，操作方便，操作模式灵活，但是炉中温度不均匀换热效果较差，出口合成气中含有大量焦油。气流床的运行温度较高，炉内温度比较均匀，焦油在气流床中裂解程度较高，但气流床气化对固体原料粒径的要求较高，进入气流床的原料需要磨成很细小的颗粒，这给含有大量纤维的生物质原料的研磨提出了另外一个技术难题。而流化床气化反应器由于热容量高、原料适应性强，可以处理高含水量物质。另外，它还具有较高的传热和传质速率。流化床内生物质颗粒可与床料充分接触、受热均匀、在气化反应器内呈沸腾燃烧状态、气化反应速度快、气化效率高、气化反应器内温度高且稳定，适于连续大规模生产，因此备受重视。但流化床反应器也存在对原料的物理特性很敏感，操作不易控制，运行温度一般也较低，出口合成气中焦油含量也相当可观，且产气中CH4和CO2含量较高，一般需要后续设备来处理焦油和重整合成气等问题，使得气化系统和装置变得比较复杂。The gasification reactors (gasifiers) currently used for biomass gasification can be roughly divided into three types: fixed bed, entrained flow bed and fluidized bed. The fixed-bed gasifier has simple structure, convenient operation and flexible operation mode, but the temperature in the furnace is not uniform and the heat transfer effect is poor, and the outlet synthesis gas contains a large amount of tar. The operating temperature of the entrained bed is relatively high, and the temperature in the furnace is relatively uniform. The degree of tar cracking in the entrained bed is relatively high, but the entrained bed gasification has high requirements on the particle size of solid raw materials, and the raw materials entering the entrained bed need to be ground into very fine particles. particles, which poses another technical challenge for the grinding of biomass feedstocks containing a large amount of fibers. The fluidized bed gasification reactor can handle substances with high water content due to its high heat capacity and strong adaptability of raw materials. In addition, it has high heat and mass transfer rates. Biomass particles in the fluidized bed can fully contact with the bed material, heat evenly, and are in a state of boiling combustion in the gasification reactor. The gasification reaction speed is fast, the gasification efficiency is high, and the temperature in the gasification reactor is high and stable. It is used in continuous mass production, so it has attracted much attention. However, the fluidized bed reactor is also sensitive to the physical properties of the raw material, the operation is not easy to control, the operating temperature is generally low, the tar content in the outlet synthesis gas is also considerable, and the content of CH4 and CO2 in the produced gas is relatively high. Generally, follow-up equipment is required to deal with problems such as tar and recombined synthetic gas, which makes the gasification system and equipment more complicated.
通过分段处理生物质原料以提高产气中合成气的浓度，降低产气中CH4和CO2含量及降低焦油含量是解决流化床反应器制备高品质合成气要求的方法之一。生物质固体首先在300～600℃左右这种较低的温度下通过热裂解制备生物质高产率的焦炭(半焦)和裂解气体，然后将热解产生的焦炭(半焦)送往流化床气化反应器中与水蒸汽一起进行高温(700～900℃)气化反应来制备粗合成气，未完全反应的焦油及制得的粗合成气再经过催化裂解(重整)床层进一步在催化剂的作用下发生焦油裂解及粗合成气重整反应来提高合成气的品质。It is one of the methods to solve the requirement of high-quality syngas production in fluidized bed reactors by treating biomass raw materials in stages to increase the concentration of syngas in the produced gas, reduce the content of CH 4 and CO 2 and reduce the content of tar in the produced gas. Biomass solids are first prepared by pyrolysis at a relatively low temperature of about 300-600°C to produce coke (semi-coke) and cracked gas with high yield of biomass, and then the coke (semi-coke) produced by pyrolysis is sent to the fluidized The high-temperature (700-900°C) gasification reaction is carried out together with water vapor in the bed gasification reactor to prepare crude synthesis gas, and the incompletely reacted tar and the crude synthesis gas produced are further processed by catalytic cracking (reforming) bed layer. Under the action of the catalyst, tar cracking and crude synthesis gas reforming reactions occur to improve the quality of synthesis gas.
把生物质通过热解、气化、催化裂解/重整分段反应转化为清洁的二次能源，可以取得双重的有效效果，一是可以解决环境污染问题，二是可以减少对石油煤炭资源的依赖，为建设资源节约型社会和环境友好型社会起到积极作用。Converting biomass into clean secondary energy through pyrolysis, gasification, catalytic cracking/reforming staged reactions can achieve double effective effects. First, it can solve the problem of environmental pollution, and second, it can reduce the impact on oil and coal resources. Dependence, and play an active role in building a resource-saving and environment-friendly society.
发明内容 Contents of the invention
本发明的目的在是要克服现有生物质制备合成气技术的缺陷，提出一种简单、高效、节能的三段式生物质热解气化制取合成气的气化装置。The purpose of the present invention is to overcome the defects of the existing technology for producing synthesis gas from biomass, and propose a simple, efficient and energy-saving three-stage biomass pyrolysis gasification gasification device for producing synthesis gas.
本发明通过下述技术方案来实现：The present invention is achieved through the following technical solutions:
本发明的主体为反应炉，采用圆柱形或方形结构，其内部上段热解炉膛为生物质热解反应室，主要以产焦炭为目的；下段气化炉膛为热解产物的水蒸汽流化气化室，主要发生焦炭(半焦)的水蒸汽气化反应，生成高品质合成气；而反应炉的中部炉膛设有环状的催化剂床层(催化裂解/重整反应室)，主要发生少量焦油的催化裂解及粗合成气的气体重整反应，以提高产气中合成气体的比例，降低焦油、甲烷和CO2的含量。所述上段热解炉膛设有进料装置，上段热解炉膛与下段气化炉膛连通。下段气化炉膛底部设置有混合气进气口。反应炉炉体上端设置有烟气出气口，烟气出气口连接有旋风分离器。反应炉外侧与上段热解炉膛、下段气化炉膛、催化剂床层对应分别设置有控温装置。The main body of the present invention is a reaction furnace, which adopts a cylindrical or square structure. The upper part of the pyrolysis furnace is a biomass pyrolysis reaction chamber, mainly for the purpose of producing coke; the lower part of the gasification furnace is a steam fluidized gas of pyrolysis products. In the chemical chamber, the water vapor gasification reaction of coke (semi-coke) mainly occurs to generate high-quality synthesis gas; while the middle furnace of the reaction furnace is equipped with a ring-shaped catalyst bed (catalytic cracking/reforming reaction chamber), which mainly produces a small amount of Catalytic cracking of tar and gas reforming reaction of crude synthesis gas to increase the proportion of synthesis gas in the produced gas and reduce the content of tar, methane and CO2 . The upper pyrolysis furnace is provided with a feeding device, and the upper pyrolysis furnace communicates with the lower gasification furnace. A mixed gas inlet is provided at the bottom of the gasification furnace in the lower stage. The upper end of the reaction furnace body is provided with a flue gas outlet, and the flue gas outlet is connected with a cyclone separator. The outer side of the reaction furnace is respectively provided with temperature control devices corresponding to the upper pyrolysis furnace, the lower gasification furnace and the catalyst bed.
所述上段热解炉膛设有的进料装置可以是：生物质料斗连通螺旋进料器，螺旋进料器通过下段下料管与上段热解炉膛连通，并且在下料管的一侧设置有氮气进气管，保证生物质物料能在氮气流的作用下顺利下落到生物质热解室中。同时螺旋加料装置外部设置有水冷装置，以保证生物质物料在进料过程中不会被加热而提前发生热解反应，从而保证生物质物料进料的通畅。The feeding device provided with the upper section of the pyrolysis furnace can be: the biomass hopper is connected to the screw feeder, and the screw feeder is connected to the upper section of the pyrolysis furnace through the lower feeding pipe, and nitrogen gas is provided on one side of the feeding pipe. The air inlet pipe ensures that the biomass material can smoothly fall into the biomass pyrolysis chamber under the action of nitrogen flow. At the same time, a water cooling device is installed outside the screw feeding device to ensure that the biomass material will not be heated during the feeding process and pyrolysis reaction will occur in advance, so as to ensure the smooth feeding of the biomass material.
所述的上段热解炉膛中间段可设置一渐缩圆锥形管段，与上端管壁形成的夹角为45°，以保证生物质物料在热解过程中顺利下落。The middle section of the upper pyrolysis furnace can be provided with a tapered conical pipe section, and the angle formed with the upper pipe wall is 45°, so as to ensure that the biomass material falls smoothly during the pyrolysis process.
所述的下段气化炉膛下端可设置有一锥形气体扩散区，且下段气化炉膛与锥形气体扩散区中间设置有多孔陶瓷布风板，锥形气体扩散区是为了保证从预热气体进气口进入的高温混合气能够沿锥形扩散区均匀扩散开来，多孔陶瓷布风板是为了使进入炉体的高温混合气体能够均匀分布，从而保证反应物料和流化介质能在气流的作用下均匀流化。锥形气体扩散区下部与混合气体预热室相通，混合气体预热室与混合气进气口相通，混合气体预热室外部设置有温控装置，通过设置控制温度，对通入的空气和水蒸汽进行混合预热，以保证后期水蒸汽气化反应顺利进行。The lower end of the lower gasification furnace can be provided with a conical gas diffusion area, and a porous ceramic air distribution plate is arranged between the lower gasification furnace and the conical gas diffusion area. The high-temperature mixed gas entering the gas port can be evenly diffused along the conical diffusion zone. The porous ceramic air distribution plate is to make the high-temperature mixed gas entering the furnace body evenly distributed, so as to ensure that the reaction materials and fluidized medium can be controlled by the air flow. uniform fluidization. The lower part of the conical gas diffusion area communicates with the mixed gas preheating chamber, and the mixed gas preheating chamber communicates with the mixed gas inlet. A temperature control device is installed outside the mixed gas preheating chamber. The steam is mixed and preheated to ensure the smooth progress of the steam gasification reaction in the later stage.
所述的催化剂床层内可放置有固定焦油裂解及粗合成气催化重整催化剂的筛网，以保证催化剂在反应过程中能稳定地放置于固定床中。所述催化剂可以是一种也可能是多种催化剂混合物。催化剂床层中优选使用含镍催化剂。A mesh of fixed tar cracking and crude synthesis gas catalytic reforming catalysts can be placed in the catalyst bed to ensure that the catalyst can be stably placed in the fixed bed during the reaction process. The catalyst may be one or a mixture of catalysts. A nickel-containing catalyst is preferably used in the catalyst bed.
本发明装置的生物质热解反应室、水蒸汽流化气化室、催化裂解/重整反应室设置在同一炉体中，但三段炉体侧面都安装有温度传感器和温控装置，在反应过程中，可以通过设置不同反应段的温度而分别对每一段进行控温，保证反应过程中热解、气化和催化裂解/重整过程相对独立且连续进行。The biomass pyrolysis reaction chamber, steam fluidized gasification chamber, and catalytic cracking/reforming reaction chamber of the device of the present invention are arranged in the same furnace body, but temperature sensors and temperature control devices are installed on the sides of the three-stage furnace body. During the reaction process, the temperature of each section can be controlled separately by setting the temperature of different reaction sections, so as to ensure that the pyrolysis, gasification and catalytic cracking/reforming processes are relatively independent and continuous during the reaction process.
本发明与其他生物质制备合成气的装置相比，具有以下优点和有益效果：Compared with other devices for preparing synthesis gas from biomass, the present invention has the following advantages and beneficial effects:
本发明结合生物质的热解特性、生物质焦炭(半焦)的气化特性、焦油的催化裂解及粗合成气的催化重整特性，将生物质热解气化制备合成气过程中的热解段、气化段、焦油及粗合成气的催化裂解(重整)过程分开，使各个反应阶段在同一装置中不同炉段相对分开且连续进行，简化了生物质制备合成气的实验系统。生物质经过低温热解、焦炭(半焦)的高温水蒸汽气化、焦油催化裂解和粗合成气重整反应，大幅度降低焦油含量，降低产气中甲烷和CO2含量，产生适用于费托合成制备液体燃料的高品质合成气，达到清洁高效利用生物质能这一可再生能源。本发明简单、高效、节能、经济和工程实现性强，大幅度地提高了气化系统的气化效率、降低了有效合成气耗氧量、提高了整个系统的能量转化率和保证了系统的稳定性等。The present invention combines the pyrolysis characteristics of biomass, the gasification characteristics of biomass coke (semi-coke), the catalytic cracking of tar and the catalytic reforming characteristics of crude synthesis gas, and the thermal energy in the process of preparing synthesis gas by pyrolysis and gasification of biomass is The decomposition section, gasification section, tar and crude syngas catalytic cracking (reforming) process are separated, so that each reaction stage is relatively separated and carried out continuously in different furnace sections in the same device, which simplifies the experimental system for preparing syngas from biomass. Biomass undergoes low-temperature pyrolysis, high-temperature steam gasification of coke (semi-coke), catalytic cracking of tar and reforming of crude synthesis gas, which greatly reduces the content of tar, reduces the content of methane and CO2 in the gas produced, and produces suitable for waste The high-quality synthesis gas of liquid fuel is prepared by the Tropical Synthesis, so as to achieve clean and efficient utilization of biomass energy, a renewable energy source. The invention is simple, efficient, energy-saving, economical and has strong engineering realizability, greatly improves the gasification efficiency of the gasification system, reduces the oxygen consumption of the effective syngas, improves the energy conversion rate of the whole system and ensures the safety of the system. stability etc.
本发明装置具有控温方便，节能环保，运行连续，结构简单等优点，可利用秸秆、稻壳、锯末等生物质料热解制取高品质合成气。The device of the invention has the advantages of convenient temperature control, energy saving and environmental protection, continuous operation, simple structure, etc., and can produce high-quality synthesis gas by pyrolyzing biomass materials such as straw, rice husk, and sawdust.
附图说明 Description of drawings
图1是本发明的装置结构示意图。Fig. 1 is a schematic diagram of the device structure of the present invention.
附图标记说明：1、生物质料仓，2、螺旋进料器，3、进料器的下料管，4、上段热解炉膛，5、催化剂床层，6、下段气化炉膛，7、多孔陶瓷布风板，8、锥形气体扩散区，9、预热气体进气口，10、混合气(空气和水蒸汽)预热室，11、混合气进气口，12、烟气出口，13、温控装置，14、温控装置，15、温控装置，16、烟气分离器(旋风分离器)，17、出灰斗。Explanation of reference signs: 1. Biomass silo, 2. Screw feeder, 3. Feeder's feeding pipe, 4. Upper pyrolysis furnace, 5. Catalyst bed, 6. Lower gasification furnace, 7. Porous ceramic air distribution plate, 8. Conical gas diffusion area, 9. Preheating gas inlet, 10. Mixed gas (air and water vapor) preheating chamber, 11. Mixed gas inlet, 12. Smoke outlet , 13, temperature control device, 14, temperature control device, 15, temperature control device, 16, flue gas separator (cyclone separator), 17, ash hopper.
具体实施方法Specific implementation method
如图1所示，本发明的新型三段式热解气化制备合成气的装置，包括反应炉，反应炉的筒状炉衬由碳化硅材质或刚玉材质制成，反应炉包括上段热解炉膛[4]、下段气化炉膛[6]和中段内侧环状催化剂床层[5]。在上段热解炉膛[4]上部设置有螺旋加料装置，螺旋加料装置包括生物质料斗[1]、螺旋进料器[2]和进料器的下料管[3]，进料管的下料管[3]插入到热解气化装置的上段热解炉膛[4]中，下料管[3]上设有氮气入口。上段热解炉膛[4]中间段设置一渐缩圆锥形管段，与上端管壁形成的夹角为45°，以保证生物质物料在热解过程中顺利下落。上段热解炉膛[4]的下部与下段气化炉膛[6]相连通，气化炉膛[6]底部设置有一锥形气体扩散区[8]，气化炉膛[6]与锥形气体扩散区[8]中间设置有开孔率在10～30％之间的多孔陶瓷布风板[3]，锥形气体扩散区[8]底部为预热气体进气口[9]，预热气体进气口[9]与混合气体预热器[10]相连通，混合气体预热器[10]底部设置有一混合气进气口[11]。热解气化反应装置炉体中段内侧设置有环状催化剂固定床层[5]，炉体上端右侧设置有烟气出气口[12]，烟气出气口[12]连接有旋风分离器[16]，旋风分离器上部设置有烟气排放口，下部设置有出灰斗[17]。热解气化装置外侧分别设置有三段控温装置[13]、[14]和[15]。As shown in Figure 1, the novel three-stage pyrolysis gasification synthesis gas preparation device of the present invention includes a reaction furnace, the cylindrical lining of the reaction furnace is made of silicon carbide or corundum, and the reaction furnace includes an upper pyrolysis furnace [4], the gasification furnace in the lower section [6] and the inner annular catalyst bed in the middle section [5]. A screw feeding device is arranged on the upper part of the pyrolysis furnace [4], and the screw feeding device includes a biomass hopper [1], a screw feeder [2] and a feeding pipe [3] of the feeder, and the lower feeding pipe [3]. The feed pipe [3] is inserted into the upper pyrolysis furnace [4] of the pyrolysis gasification device, and the feed pipe [3] is provided with a nitrogen inlet. A tapered conical pipe section is set in the middle section of the upper pyrolysis furnace [4], and the angle formed with the upper pipe wall is 45° to ensure the smooth falling of the biomass material during the pyrolysis process. The lower part of the upper pyrolysis furnace [4] is connected with the lower gasification furnace [6]. There is a conical gas diffusion zone [8] at the bottom of the gasification furnace [6]. The gasification furnace [6] and the conical gas diffusion zone [8] There is a porous ceramic air distribution plate [3] with an opening rate between 10% and 30% in the middle, and the bottom of the conical gas diffusion area [8] is the preheating gas inlet [9]. The gas port [9] is in communication with the mixed gas preheater [10], and a mixed gas inlet [11] is arranged at the bottom of the mixed gas preheater [10]. A ring-shaped catalyst fixed bed [5] is arranged inside the middle section of the furnace body of the pyrolysis gasification reaction device, and a flue gas outlet [12] is arranged on the right side of the upper end of the furnace body, and the flue gas outlet [12] is connected to a cyclone separator [ 16], the upper part of the cyclone separator is provided with a flue gas discharge port, and the lower part is provided with an ash hopper [17]. Three-stage temperature control devices [13], [14] and [15] are installed on the outside of the pyrolysis gasification device.
该装置运行时，由螺旋进料器[2]将生物质料仓[1]中的生物质经由其下端的下料管[3]加入到上段热解炉膛[4]中，在温控装置[13]的控制下进行低温热解反应，生物质低温热解的产物主要为生物质焦炭(半焦)和裂解气体。在氮气流的作用下，热解产物不断下行至下段气化炉膛[6]中与混合气体预热器[10]中进来的水蒸汽混合气体发生高温水蒸汽气化反应，气化温度通过温控装置[15]来控制，混合气体进气流量通过质量流量计来控制，使炉内热解焦炭(半焦)及流化介质处于流化状态，使气化反应充分进行，而气体预热器[10]进来的预热气体通过多孔陶瓷布风板[7]进行布风，使进来的混合预热气体能够均匀分布。在此过程中，主要热解产物焦炭(半焦)进一步与水蒸汽发生水煤气反应生成粗合成气。而后热解气化后产生的少量焦油及制得的粗合成气再经由炉内侧环状催化剂床层[5]，在镍基催化剂的作用下且通过温控装置[14]进行控温，从而发生焦油催化裂解和粗合成气的水蒸气催化重整反应，生成不含焦油或焦油量很少的高品质合成气体。产生的气体携带未完全反应的少量焦炭和生物质灰渣一起通过烟气出口[12]进入旋风分离器[16]中，通过旋风分离，将产生的气体与参与灰渣进行分离，使产生的气体得以净化，灰渣收集在出灰斗[17]中进行其他应用。When the device is running, the biomass in the biomass bin [1] is fed into the upper pyrolysis furnace [4] through the lower end of the feed pipe [3] by the screw feeder [2], and the temperature control device [ 13] under the control of low-temperature pyrolysis reaction, biomass low-temperature pyrolysis products are mainly biomass coke (semi-coke) and cracking gas. Under the action of the nitrogen flow, the pyrolysis products continuously go down to the gasification furnace [6] in the lower section to undergo a high-temperature water vapor gasification reaction with the steam mixed gas coming in from the mixed gas preheater [10]. Controlled by the control device [15], the intake flow rate of the mixed gas is controlled by a mass flow meter, so that the pyrolysis coke (semi-coke) and the fluidized medium in the furnace are in a fluidized state, so that the gasification reaction is fully carried out, and the gas preheating The preheating gas coming in from the device [10] is distributed through the porous ceramic air distribution plate [7], so that the incoming mixed preheating gas can be evenly distributed. In this process, the main pyrolysis product coke (semi-coke) is further reacted with water vapor to generate crude synthesis gas. Then, the small amount of tar produced after pyrolysis and gasification and the crude synthesis gas produced pass through the annular catalyst bed [5] inside the furnace, and are controlled by the temperature control device [14] under the action of the nickel-based catalyst, so that Catalytic cracking of tar and steam catalytic reforming of crude synthesis gas occur to generate high-quality synthesis gas with no or little amount of tar. The generated gas carries a small amount of incompletely reacted coke and biomass ash through the flue gas outlet [12] and enters the cyclone separator [16], and the generated gas is separated from the participating ash through the cyclone separation, so that the generated The gas is purified and the ash is collected in the ash hopper [17] for other applications.
以上所述仅为本发明的较佳实施例，并非对本发明作任何形式上的限制；凡本行业的普通技术人员，均可按以上所述和说明书附图所示而顺畅地实施本发明；但凡在不脱离本发明技术方案而作出的更动、修饰与演变的等同变化，均为本发明的等效实施例，均仍属于本发明技术方案的保护范围。The above descriptions are only preferred embodiments of the present invention, and are not intended to limit the present invention in any form; any ordinary skilled person in this industry can smoothly implement the present invention according to the above description and the drawings shown in the description; All changes, modifications and equivalent changes made without departing from the technical solution of the present invention are equivalent embodiments of the present invention, and still belong to the protection scope of the technical solution of the present invention.
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Families Citing this family (19)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| ES2441691B1 (en) * | 2013-10-21 | 2014-08-11 | Eqtec Iberia S.L. | Procedure for the conditioning of a gas stream from a gasifier, thermal cracking of tars and steam reforming and reactor used |
| CN103937552B (en) * | 2014-03-24 | 2015-11-18 | 北京交通大学 | A kind of three-section type entrained flow bed coal hydrogenation gasification stove and combined operation system |
| CN105861058A (en) * | 2016-06-21 | 2016-08-17 | 安徽理工大学 | A kind of preparation method of clean biogas |
| CN106190203A (en) * | 2016-07-01 | 2016-12-07 | 北京神雾环境能源科技集团股份有限公司 | The preparation system of a kind of synthesis gas and method |
| CN105925321B (en) * | 2016-07-12 | 2019-07-12 | 安徽省化工设计院 | A kind of dedusting decoking integration biomass gasification stove |
| CN107043639B (en) * | 2016-10-18 | 2022-10-21 | 彭振德 | Axial counter-flow type straw chopping coupling purification hydrogen-rich gasification stove |
| CN106367119B (en) * | 2016-10-26 | 2019-04-09 | 南京大学 | A pyrolysis and biomass gas catalytic reforming reactor and its application |
| CN106367122A (en) * | 2016-11-29 | 2017-02-01 | 河南农业大学 | Device and method for preparing synthetic gas by gasification of biomass carrier of oxygen |
| CN108735399B (en) * | 2018-05-21 | 2020-11-03 | 阙南平 | Continuous treatment equipment for waste circuit boards/waste enameled wires based on pyrolysis liquation principle |
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| CN110749719A (en) * | 2019-09-02 | 2020-02-04 | 宁夏大学 | Visual experiment system for coal coke and slag wall surface reaction |
| CN110923015B (en) * | 2019-12-09 | 2021-05-14 | 万华化学集团股份有限公司 | Pyrolysis-gasification integrated treatment device and method |
| CN111269735B (en) * | 2020-01-21 | 2021-03-02 | 中国特种设备检测研究院 | A biomass three-stage pressurized high temperature pyrolysis gasification device |
| CN112251260B (en) * | 2020-11-05 | 2022-07-12 | 北京衡燃科技有限公司 | Overhead feeding TFB gasification furnace |
| CN114479953B (en) * | 2022-01-27 | 2023-03-21 | 华中科技大学 | Device for preparing synthesis gas by utilizing biomass |
| CN117106489B (en) * | 2023-10-23 | 2024-02-20 | 西子清洁能源装备制造股份有限公司 | Device and method for producing synthetic gas by three-stage pyrolysis and gasification of organic solid waste |
| CN118374300B (en) * | 2024-04-22 | 2025-01-28 | 南京林业大学 | Biomass carbonization coupled with volatile steam reforming to produce carbon-hydrogen |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN2055503U (en) * | 1989-07-08 | 1990-04-04 | 清华大学 | Single-stage fluidized bed powder coal gasified furnace |
| CN101407724A (en) * | 2008-10-27 | 2009-04-15 | 合肥天焱绿色能源开发有限公司 | Vertical combined gasification furnace for solid biomass |
Family Cites Families (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4968325A (en) * | 1987-08-24 | 1990-11-06 | Centre Quebecois De Valorisation De La Biomasse | Fluidized bed gasifier |
| CN2461925Y (en) * | 2001-02-13 | 2001-11-28 | 王同章 | Circulating fluidized bed gasification furnace |
| JP2004182903A (en) * | 2002-12-04 | 2004-07-02 | Kawasaki Heavy Ind Ltd | Biomass gasification method and gasification apparatus |
| CN2677376Y (en) * | 2004-01-16 | 2005-02-09 | 中国科学院广州能源研究所 | Down-draft gasification furnace |
| JP4546862B2 (en) * | 2005-03-25 | 2010-09-22 | メタウォーター株式会社 | Circulating flow type gasifier |
| CN101245264B (en) * | 2008-03-25 | 2011-02-16 | 东南大学 | Single-bed self-heating type thermal decomposition gasification combustion reactor and thermal decomposition gasification combustion method |
| CN101747943B (en) * | 2008-12-01 | 2013-01-16 | 中国农业科学院农业环境与可持续发展研究所 | Method by utilizing livestock manure to produce hydrogenous gas and other products in a step-by-step thermal decomposition way and device |
| CN102021038B (en) * | 2009-09-14 | 2012-10-10 | 新奥科技发展有限公司 | Multilayer fluidized bed gasification furnace for preparing methane-rich gas by coal gasification |
-
2011
- 2011-08-26 CN CN201110249081.5A patent/CN102329651B/en not_active Expired - Fee Related
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN2055503U (en) * | 1989-07-08 | 1990-04-04 | 清华大学 | Single-stage fluidized bed powder coal gasified furnace |
| CN101407724A (en) * | 2008-10-27 | 2009-04-15 | 合肥天焱绿色能源开发有限公司 | Vertical combined gasification furnace for solid biomass |
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